Saponification of fats and oils



Nov. 19, 1940. M. H. rr'rNER 2.221,799

SAPONIFICATION OF FATS AND OILS Filed April 22, 1937 3 Sheets-Sheet 1 1 ,f5y 6 Je l INIVENTOR .34

Nw. 19, 1940. M HQ ,TTNER 2,221,799

SAPONIFICATION OF FATS AND OILS Filed April 22, 1937 :s sheets-sheet 2 Nov. 19, 1940. M H, r11-NER 2,221,799

SAPONIFIGATION 0F FATS lANI) OILS ned April 22, 19:57- :5 sheets-sheet :s

ATTORNEYS Patented Nov. 19, 1940 UNITED STATES PATENT OFFICE SAPONIFICATION 0F FATS AND OILS Application April z2, 1937, semi Np. 138,311

ze emma (c1. 26a- 415) This invention relates to an improved process and apparatus for the aqueous saponification or hydrolysis of fats and fatty oils to produce fatty acids and glycerin.

It is an object of the present invention to provide an improved process and apparatus for splitting or hydrolyzing fats and fatty oils, which are largely triglycerides, into fatty acids and glycerin, with the production of aqueous glycerin and relatively pure fatty acids uncontaminated by decomposition products or tars or by catalytic materials or reaction products of catalytic materials.

It has been proposed heretofore to accomplish the aqueous hydrolysis of fats and fatty oils by heating the fats or fatty oils together with liquid water at comparatively high temperatures, and at pressures sufficient to prevent the formation of steam in contact with the mixture being heated, with the production of an aqueous solution of glycerin and fatty acids. Usually in such processes, a small amount of a catalyst, such as lime, `magnesia, or other basic material, or sulfuric acid or other acid, or the so-called Twitchell reagents, has been used to accelerate the reaction, although processes in which no catalyst is used but'in which the saponication or ,hydrolysis is used but inwhich the saponiflcation or hydrolysis is effected by water alone have been proposed or used to some extent.

In general, such processes as have been used or proposed heretofore result in balanced reactions which go to equilibria, and the saponication or hydrolysis is incomplete, except with repetitions of the treatment. In such processes, the saponiflcation or hydrolysis seldom proceeds as far as completion, except under extremely favorable conditions. By removing the aqueous solution of glycerin formed and subjecting the fatty matter to repetitions of the treatment, the saponification or hydrolysis may be brought up to of completion, or, under favorable conditions, somewhat higher.

It has been proposed to carry out these processes of 'aqueous saponication or hydrolysis in several different ways, as by agitating the fat or fatty oils with water inan autoclave at high temperatures and pressures, or by passing the water and fat or fatty oil concurrently through a tube or coil. Such methods of carrying out the saponication or hydrolysis are, of course, equivaient in that they all result in the balanced reaction tending to go to an equilibrium, and the same degree of saponification is obtained by these various modifications of these processes provided the proportions of materials, the temperatures and the pressures are the same and sunlcient time is allowed to reach an equilibrium.

, As an illustration of the fact that these hy- 5 drolyses or saponiiications as commonly carried out are balanced or reversible reactions which do not go to completion even at high temperatures and pressures, I have determined that if a mixture containing 35 parts of pure neutral tallowlO and 25v parts of pure water is heated under pressure in an autoclave to about 255 C. for about 3 hours, or until an equilibrium is reached, a product is obtained which is about 92% hydrolyzed. If a mixture containing glycerin and pure tallow fatty acids, in the exact amounts which would be obtained by complete hydrolysis of 35 parts of pure neutral tallow, and sumcient water to make the tota.l.60 parts is heated in an autoclave to-255 C. for 3 hours and at the same 20 pressure as employed in the test described above, an esteriflcation takes place with the formation of glycerides and with the production of a mixture about 92% hydrolyzed. Thus the same equilibrium is arrived at whether neutral tallow 25 and water are heated together, or whether tallow fatty acids, glycerin and water are heated together. Similar experiments with cocoanut oil indicate that the same phenomenon occurs, except that a larger proportion of water is required 30 for the same degree of hydrolysis. t lower temperatures and pressures, longer periods are required for. the reaction to reach an equilibrium point, at equilibrium the hydrolysis is con' siderably less. 35

When such processes are modified by the addition of catalysts, the final equilibrium reached is not materially affected, as the catalysts merely cause the reaction to reach the equilibrium in a shorter period of time.

In my prior application Serial No. 83,991 flled June 6, 1936, I have described a process for the aqueous sapcniflcation of fats and fatty oils which results in substantially complete aqueous saponication. In the process therein described, the

fat or fatty oil is brought into countercurrent contact with liquid water at temperatures around 250 C. and pressures sumcient to maintain the aqueous phase in a liquid state. In said process, 50

the essential limiting conditions are the use of temperatures sufliciently high so that the solbility of the water in the fatty material is in excess of the amount required for complete saponification but below the temperature at which the u fatty material and the water tend to merge into a single phase, that is, in general below about 287 C. and the use or pressures above the pressure cf saturated steam at the highest tempera- 5 ture employed, to prevent Vaporization. Sufllcient excess wate. must be supplied to provide that which dissolves in the fatty material at the high temperatures employed, that required for the hydrolysis or saponilcation, and that required to'wash out the glycerin; and the process effects the substantially complete aqueous saponiy cation of the fatty material with the production of a relatively concentrated and pure glycerin.

'I'he present invention provides a new and improved process permitting the aqueous hydrolysis or saponiiication of fats or fatty oils with the production of relatively concentrated aqueous glycerin and fatty acids uncontaminated by catalysts' or other objectionable impurities requiring special treatment for their removal, the new process thus having many of the advantages of the process of my said prior application, but differing therefrom in important respects.

In accordance with the present invention, the saponification or hydrolysis is carried out in two operations, advantageously portions of a single continuous process, the firstI of which results in the hydrolysis of a substantial proportion of the fatty material, advantageously setting free 80 90% of the fatty acids, by a balanced or equilibrium reaction accomplished by the concurrent heating of the fatty material in contact with water ordilute aqueous glycerin and the second of which involves the substantially complete saponication of the fatty material separated from the aqueous glycerin after the first operation by subjecting the separated and partially sapcniiied fatty material to countercurrent contact with water or with successive portions of water, continuously or intermittently; at a temperature suiliciently high to insure relatively rapid reaction, e. g. temperatures in excess of 200 C., but below the temperature at which a single phase would result with the amount of water taken, that is,

below a temperature of about 287 C., and at pressure sufficiently high to prevent the vaporization .of the water.

rst operation is the relatively dilute aqueous glycerin resulting from thev nal or countercurrent saponiflcation or hydrolysis, as I have found `that the balanced or equilibrium reaction which takes place between water and fatty material at high temperatures and pressures in a batchor concurrent flow operation is not materially aifected, if instead of water a dilute aqueous glycerin solution, containing, for example, about 15% or less of glycerin, is'used. While the presence of this amount of glycerin in the water used for this initial operation may affect the degree of saponication obtained to the extent of reducing the percentage of free fatty acids set free by a small amount, it does not materially affect the operation of the process, and it enables the pro-- duction of substantially all of the glycerin separated from the fatty material in the form of a relatively concentrated glycerin solution which may contain up to 30% of more glycerin.

I have found, for example, that if, under certain conditions of temperature and pressure, an equilibrium with about 92% of complete saponication is obtained in the presence of a nal glycerin solution containing about 15% glycerin,

Advantageously, the aqueous liquid used in the' similar material under vsimilar .conditionsqgwill result in about 87% of complete saponification if an amount of glycerin is present that will give a nal glycerin solution in contact with the fatty matter containing about 30% glycerin.

In the initial operation, that is, the operation involving the concurrent contact of the water or dilute aqueous glycerin with the fatty material, it is not necessary to maintain the temperature below that at which a singlephase results duringthe entire' operation, but it isimportant to maintain the temperature suiliciently high, e. g. above about 200 C., to insure a fairly rapid reaction so that the equilibrium is approached within a reasonable time, or so that a substantial de-l grec of hydrolysis is obtained within a reasonable time, and to maintain the temperature of the fatty material and aqueous glycerin substantially below 287 C. when the separation of the fatty material and the aqueous glycerin iscarried out so as to insure the presence of an aqueous phase and a fatty'phase capable of separation.

An advantageous way of carrying out the initial saponiflcation involves passing dilute aqueous glycerin, containing about 4% of glycerin, for example, concurrently with fatty material in the proportions of about 8 parts by weight of fatty material to 5 parts by weight of the aqueous glycerin through a tube or pipe in which the mixture is heated to a temperature of about 250 C. or somewhat higher under a pressure substantially above the pressure of saturated steam at that temperature and discharging the `mixture into a reservoir or quiet zone also maintained at a high temperature and pressure, in which the undissolved water and glycerin separate by subsistence as a glycerin solution containing approximately 15% glycerin. This glycerin solution may be drawn out through a suitable outlet at the bottom of this vessel and separated from the fatty material, which will contain about 90% free fatty acids if the time of contact between the aqueous liquid and the fatty material at the temperature indicated has been about one hour. The aqueous glycerin which is removed at the high temperature contains a few percent' of dissolved fatty material, and it is advantageously introduced into another pressure vessel,

while the high pressure is maintained, in whichv it may be cooled to about C. with the result that the dissolved fatty material separates and may be returned to the rst vessel. 'I'he aqueous glycerin may then be removed from thegsecond pressure vessel through suitable outlets and thus be obtained as a glycerin solution substantially free from fatty material.

The partially 'saponiiled fatty material in the rst pressure vessel, which may advantageously contain about 90% free fatty acids, is forced out of the top of the vessel by the constant inflow of new fatty material and aqueous glycerin into the bottom of another pressure vessel through which it passes upwardly in countercurrent contact with water under `a suitable high temperature and pressure and in which the saponilcation or hydrolysis is substantially completed, with the result that the fattymaterial, may b'e withdrawnA from the top of the countercurrent' vessel in the form of free fatty acids containing substantially no glycerin and containing no water except that dissolved. By cooling the fatty material before the removal from the countercurrent vessel, as by introducing cold water instead of heated water at the top to effect the countercurrent saponication, the fatty acids which are removedmay and water, as the solubility of water in the fatty material at temperatures of about 185 C. or lower is very slight.

At the bottom of the countercurrent pressure vessel the aqueous glycerin resulting from the reaction is separated from undissolved fatty material as a solution containing about 4% glycerin, and this solution is yadvantageously used in the initial saponiiication by simply pumping it, while maintaining the high pressure, to the initial heating coil, where it is admixed with the fresh fat or fatty oil to be treated.

The initial heating coil, in which the fat or fatty oil and water or aqueous glycerin is first heated to the high temperatures and pressures may advantageously be so heated that the temperature of the material passing through it is somewhat greater than that maintained in the reservoir into which it discharges, which must be kept at a temperature substantially below about 287 C. I have found that the rate of saponiiication increases rapidly as the temperature is increased, and that by maintaining the temperature of the heating coil somewhat above the temperature of the pressure vessel into which it discharges the rate of saponicationcan be increased, and the constant discharge of the material, heated to a temperature somewhat in excess of that maintained in the pressure vessel, into the pressure vessel serves to neutralize the heat losses from the pressure vessel and to aid in maintaining its temperature at the desired point.

In this operation as described, it will be seen that the water employed first passes in countercurrent contact with Ithe partially saponiiled fatty material and then is used for the initial saponification of the fat or fatty oil and is removed as comparatively concentrated glycerin solution after this initial saponiiication, while the fat or fatty oil is first subjected to an initial saponiflcation by concurrent contact with dilute aqueous glycerin and subsequently, after partial saponication or hydrolysis, to countercurrent contact with fresh water, after which it is obtained as fatty acids containing substantially no combined glycerin. In the operation described, the fat or fatty oil and the water have been indicated to be used in the relative proportions by weight of about 8 to 5, and the glycerin solution nally obtained contains about 15% glycerin, but the proportions of fatty material and water used can be widely varied with the production of glycerin solutions of lower or higher concentrations than indicated, glycerin solutions containing as -much as 30% of glycerin or more being readily obtainable.

As has been pointed out, the initial hydrolysis is an equilibrium reaction, involving a time factor for the `attainment of a substantial degree of hydrolysis, and advantageously it is carried to substantial equilibrium so that most of the hydrolysis is accomplished in this operation and the 65 sizeo'f the vessel required for the final countercurrent hydrolysis may be relatively small, or conversely, the capacity of a given vessel may be relatively high. To provide this time factor, I may provide a pressure vessel of large cubic capacity into which the coil in which the water or dilute aqueous glycerin and fatty material is heated discharges. This pressure vessel should be so constructed that it can be maintained at the high temperature and pressure employed, and should advantageously have a capacity somewhat vin excess ofthe volume of fat that is to be treated during the time that it is necessary for lthe saponifying action to approach an equilibrium. Thus if 2500 pounds of fat are to be saponifled in one hour and the equilbrium is approached in about 50 minutes, which is about the time required if a temperature of about 260 C. is used, it is advantageous to provide a pressure vessel having a size sufficient to hold I2500 pounds of hot fatty material in addition to the water or glycerin solution that is present.

It is not necessary that this reservoir be -a separate-pressure vessel, as the hot mixture of partially saponiiied fatty material and glycerin solution may be discharged from the heating coil directly into the bottom of the countercurrent saponifying pressure vessel and the separation of the fatty material from the glycerin solution may be eifected in a suitable zone provided in the bottom of this vessel, particularly if the heating coil is ,quite long and is heated to a relatively high temperature, so that -a substantial amount of saponication takes place in it.

The invention will be further illustrated by reference to fthe attached drawings, which illustrate, in a diagrammatic and conventional. fashion, apparatus embodying the invention and adapted for use in carrying out the process of the invention. i

In the drawings,

Fig. 1 illustrates diagrammatically one form of apparatus suitable for carrying out the process of the invention and which embodies the invention provided with a separate .reservoir or pressure vessel for providing the necessary time factor in the initial saponiflcation; and

Fig. 2 illustrates diagrammatically a modified form of the apparatus which embodies the invention and which is suitable for carrying out the process', in which the zone in which the initial saponiflcation is completed is included within the pressure vessel in which the final countercurrent saponication is carried out.

Fig. 3 illustrates diagrammatically a modified form of a portion of the apparatus of Fig. l.

In Fig. l there is shown a heating coil l of suitable corrosion and pressure resistantA material into which the fatty material to be saponified is introduced through inlet I2 by pump I4 and water or dilute aqueous glycerin through inlet I6 by pump I8. This heating coil is heated by means of diphenyl oxide or other suitable heating medium introduced into the jacket 20 and should be sufficiently long to insure that the material passing through it is heated to the high temperatures used, e. g., it may be made from about 50 feet of suitable tubing. This heating coil discharges through pipe 22 into the pressure vessel 24, also made ofa suitable corrosion resistant material, which should be of such a size as to hold a quantity of hot fatty material equal to that to be saponified during the period' required for the initial saponification to be carried out to the desired extentlas well as the aqueous glycerin which may be present. Eor example, if 2500 pounds of fatty material are to be saponifled per hour and if the period required for the initial saponiflcation to proceed to the desired extent is about 50 minutes, the capacity of this pressure vessel should be about 2500 pounds of hot fatty material plus the aqueous glycerin which may be present so that the period during which the initial saponification is carried out is somewhat in excess of the 50 minutes required for the approximate equilibrium to be reached.

4 y This pressure vessel is kept substantially full of fatty material, with a small layer of aqueous glycerin at the bottom, and is advantageously provided with petcocks 26 or other suitable lndicating means to enable the -determination of the position ofthe interface .between the aqueous glycerin and the fatty material. At the bottom of this pressure vessel is provided an outlet 28 through which the aqueous glycerin is wither weight, rises upwardly through thepipe 32 which extends from the top of the pressure vessel 30 into the pressure vessel 24 to above the level of the interface between the aqueous glycerin and the fatty material in vessel 24. By providing this means vof withdrawing the aqueous glycerin and returning the fatty material dissolved therein to the pressure vessel 24,- the aqueous glycerin can be withdrawn from the vessel 30 through the outlet 344 substantially free from both dissolved and undissolved fatty material. The vessel 38 may be provided with petcocks or other suitable devices to enable the withdrawal of samples, to make sure that the material withdrawn is aqueous glycerin, and to enable the adjustment of the rate of withdrawal to avoid the withdrawal any fatty material.

The vessel V24 is provided at the top with an outlet 38 which discharges somewhat above the bottom of the pressure vessel 48 in which the countercurrent saponication is carried out. By introducing the partially saponiiied fatty mate- 40 rial from the vessel 24 somewhat above the bottom of the vessel 40 there is provided at the bottom of this vesselel settling zone 4I in which the fatty materials may be separated by gravity from the water and aqueous glycerin which flows downwardly through the vessel 48. Petcocks 42 or other suitable devices may be prorate of withdrawal of the aqueous glycerin' vided to enable the determination of the interface between the fatty material and the aqueous glycerinin this zone of the vessel 40, so that the through the outlet 44 may be adjusted to keep this interface below the point of introduction of fatty material through the pipe 38, the vessel 40 thus being kept substantially full of fatty material except for the water and aqueous glycerin flowing downwardly through it and that in the zone 4I at the bottom.

'I'he interior ofthe pressure vessel 4|Il above the' settlingzone at the bottom is advantageously provided with means to cause the material passing through thevesselto follow labyrlnthian paths. One suitable construction yis shown in Fig. 1, the `parts not being to scale. The vessel 48 may be, for example,` about 2 feetin diameter and "15 feet high, for .operation in cooperation with a pressure vessel designed to hold about 2500 pounds of hot fatty material, as described above, and made of suitable pressure resistant and corrosion resistant materials, such as stainless steel.,l y.It is shown as provided with a series of trays 48 and 48 with the alternate trays 46' ple, about one inch apart, more or less, but are shown as proportionately further apart, for convenience of illustration. The trays are suitably supported by rods or other devices (not shown) and are so constructed and arranged as to cause the material to follow labyrinthian paths, to increase the efficiency of the excess liquid water in washing out glycerin from the fatty acids.

'I'he alternate trays 48 are shown as of materially less diameter than the inner diameter of the vessel and as provided with rims at their outer peripheries over which the material flowing downwardly, that is, the aqueous glycerin or water, must flow; while the other trays 46 which are shown as having the same diameter as the inner diameter of the vessel, but which may advantageously have a somewhat smaller diameter to allow for clearance and expansion, are also provided with outer peripherial rims and with openings at the center with somewhat lower rims over which the water'or glycerin must flow in its downward path. The fatty material, rising through the vessel, follows a reverse path.

At the top of the vessel 40 there is provided another separating zone 50 for the separation of the outgoing fatty acids from undissolved water or aqueous glycerin. These fatty acids, which are substantially completely saponied after the passage through the vessel 48 are removed from the top thereof through the outlet 52. Water is introduced at a point somewhat below the top of the pressure vessel 40 through the inlet 54, this inlet extending suiciently far down into the vessel to provide the separating zone at the top. The water which is thus introduced may be either cold or not, but of course is under a high pressure. If cold water is introduced, the fatty acids which emerge from the vessel-are relatively cool, so that they contain little or no dissolved water or glycerin; whereas if water at a. high temperature is introduced, the fatty acids which emerge may contain as much as 20% or more dissolved water.

The pressure vessel 40 may be provided at suitable places with petcocks 56 for sampling purposes. i

As previously described, the aqueous glycerin removed from the vessel 40 flows out through the A erin is removed through the pipe 58 and used for other Purposes, water may be used in the initial saponiiication, being introduced through the pipe 62. Suitablevalves 64 are provided to permit this glycerin solution removed from the vessel 40 to be used in these various ways, it being understoodl that the system is suiilciently flexible so that part or all of this glycerin solution may be removed 'through the pipe 58 and part or all of it may be used for the'initial saponication,

supplemented if desired, by water introduced through the pipe 62.

Suitable gauges 63 for determining the pressure at the various parts of the apparatus are provided. as is a safety valve 65 which may be 1ocated on the pipe 44 or in another place as desired. It is to be understood that the entire apparatus, with the possible exception of the vessel `3l), is to be suitably and efciently insulated to conserve heat, and if necessary, suitable external unitary heaters or jackets are to be applied to the various portions of the apparatus to replace heat lost through radiation and to supply heat and control heating. For example, it may be found necessary to provide unitary heaters or a heating jacket around the vessel 40 to insure the maintenance of the necessary high temperature in this vessel, at least toward the bottom and intermediate portions in which substantially all of the final saponiiication takes place. And this is true particularly Where cold water is introduced through the pipe 54, as this cold Water rmust be heated up to the proper reaction temperature, which is above about 200 C., in order to insure the completion of the saponifcation.

An advantageous method of operating this apparatus consists in introducing fatty material to be saponiiied through the pipe I2 and simultaneously introducing cold water through the pipe 54, the fatty material and water being used in proportions of about 8 to 5 by weight. After the process has proceeded through the initial stages and is operating normally, dilute aqueous glycerin containing about 4% glycerin is withdrawn from the bottom of the pressure vessel 40 and is introduced through the pipes 44, 60 and I6 and the circulating pump I8 into the heating coil I along with the fatty material introduced through the pipe I2 and the pump I4. In this heating coil, the admixed materials are raised in temperature to about 250 C., or advantageously somewhat higher, for example, to about 265 C., under a pressure sufficient to prevent the formation of a vapor phase. After being heated in this coil, the admixed materials are discharged through the pipe 22 into the pressure vessel 24, in which the temperature maintained may advantageously be about 250 C., and is advantageously somewhat below the temperature of the heating coil I0, so as to insure the maintenance of a fatty phase and an aqueous phase in this vessel while at the same time maintaining the solubility of the water in the fatty material at a sufficiently high point to insure that the saponiiication proceeds with reasonable rapidity. If desired, an agitator may be provided in this vessel 24 to promote the intimacy of contact between the fatty material and the aqueous liquid. One or more insulated pressure vessels' similar to 24 may be employed in series with 24 if desired for the purpose of increasing the hot storage of partially saponied fatty material and for theavoidance of short circuiting. These vessels may advantageously be so arranged and so connected that any aqueous glycerin solution separating from the fatty matter due to reduction in temperature and lessened solubility of water in the fatty matter, vlwill flow backward and eventually find its way into the vessel 24 and vessel 30, as hereinafter described in connection with Fig. 3. It will also be noted that in the 1 w advantageous operation described, the temperature in the heating coll is above thatin the pressure vessel, so that the heat introduced by the highly heated`material from the heating coil` serves to neutralize the heat loss by radiation from the pressure vessel 24 so that it may be unnecessary to supply additional heat to this vessel. In this pressure vessel, the initial saponiflcation proceeds almost to an equilibrium, and aqueous glycerin separates by subsistence at the bottom oi the vessel, the interface between this aqueous liquid and the fatty material being determinable by the petcocks 26 or other suitable devices. 'Ihe aqueous liquid iows downwardly through the outlet 28 into the vessel 3l, the flowbeing controlled by a valve on the pipe 34 (not shown).

In this vessel, the aqueous glycerin is cooled, advantageously to about 100 C., with the result that the dissolved fatty material, which may amount to about 5% at the high temperature of 250 C., separates and rises to the top of the vessel and then flows upwardly through the pipe 32 and is returned to the pressure vessel 24. The fatty material which is partially saponied and which collects at the top of the pressure vessel 24, nearly filling this vessel, is forced upwardly through the pipe 38, by the incoming fatty material and aqueous liquid, into the pressure vesselA 40, which it enters somewhat above the bottom -and above the separating zone which is provided there. The partially saponied material then flows upwardly through the pressure `vessel 40, following the labyrinthian paths required by the trays or other devices provided in this vessel, thus flowing countercurrently to the water which is introduced through the pipe 54 in the proportions referred to above. The water if not preheated is heated by the upwardly flowing fatty material (this heating may be supplemented by providing a heating jacket or heaters around the exterior of the vessel 40), and al temperature of about 245-250 C. is maintained in this vessel, this temperature being suiiiciently high to insure' that the fatty material dissolves suiiicient Water to provide that required for the completion of. the saponiiication, that dissolvedA in the fatty material, but sufficiently low to insure an aqueous phase of sufficient volume to wash out the glycerin as a dilute aqueous glycerin with the proportions of water and fatty material selected. The Water ows downwardly and collects in the zone providedl at the bottom of this vessel as dilute aqueous glycerin containing about 4% more or less glycerin, while the fatty material flows to the top-of the vessel where it is cooled by the incoming water orK otherwise, and where substantially all of the dissolved Water separates out, so that the fatty acids removed from the top of the vessel through the pipe 52 are substantially free from dissolved water. Of course, if hoil water is introduced through the inlet 54, the fatty acidsl will not be cooled to such an extent, and when removed will contain considerable proportions of dissolved water.

Using the proportions described, the aqueous glycerin which is finally removed from the vessel 30 will contain 15 to 20% of glycerin, depending upon the nature of the fatty material used; if tallow be the fatty material, for example, the aqueous glycerin will contain about 15% glycerin, whereas if cocoanut oil is used, the aqueous glycerin. will contain a somewhat higher percentage of glycerin. These proportions of fatty material and water, that is, 8 parts of fatty material to 5 parts of water, are advantageous, but they may be varied widely. In general, the amount of water, in the aqueous glycerin or as water, used in the initiaLconcurrent saponiiication should be in excess of about 10% of the weight of the fatty material, and advantageously is in excess of about 30% of the weight of the fatty material. Good results are obtained when the final glycerin solution contains around glycerin, but by using less water, more concenobtained.

It will be noted that throughout the entire operation, the pressure maintained upon the liquid is`approximately the same, and this pressure should be sufficiently high to prevent any vaporization with the highest temperatures employed in the process, which ordinarily are the'.

necessary that separatel fatty and aqueous phases be maintained in the heating coil, as the saponilcation proceeds so long as the temperature is sufficiently high to insure a substantially high solubility of the water in the fatty material, whether the water and :fatty material be present in two phases, or whether the temperature be sufliciently high so that the two phases merge into a single phase. It is important, of course', that the temperature in the pressure vessel 2d be substantially below that at which a single phase is formed, so that separation of the aqueous glycerin from the fatty material can take place, a temperature of from 200 to about 250 C., or even a little higher, in this vessel being advantageous. Similarly, it is important that the temperature in the countercurrent pressure vessel 50 be maintained well below the temperature at which a single phase is formed, so that the countercurrent flow of the water or aqueous glycerin and fatty material can take place, temperatures ranging from 200 C.A up to about 250 C. or a little higher in this vessel being advantageous, The temperatures which may be used in the pressure vessel 213 and the countercurrent vessel 40 may be varied quite widely within the ranges described above, the higher temperatures giving increased rates of saponication due largely to increased solubility of the water in the fatty material, but at the same time requiring the use of somewhat more water to provide that needed to wash the glycerin from the fatty material after saponiiication. Even lower temperatures, e. g., temperatures ranging down to about 185 C. may be used in various parts of the apparatus, but at such lower temperatures the reaction is quite slow, and the capacity' of the apparatus is greatly decreased.

In Fig. 2 there is illustrated a modified form of apparatus which is also suitable for carrying out the process. In this form of apparatus, instead of providing a separate pressure vessel into which the heating coil in which the water and fatty material is initially heated discharges, the heating coil discharges into the bottom of a large pressure vessel 10 somewhatabove the bottom thereof, into the zone 12, which thus forms a reservoir more or less comparable to the pressure vessel 24 of the apparatus of Fig. 1. Suitable petcocks or other devices 14 are provided here to permit the determination of the interface'between the fatty material andthe aqueous glycerin. In this form of apparatus it is advantageous to have the heating coil 16 somewhat longer thanthat of the apparatus of Fig. 1, so `that the period of contact lbetween the water and the fatty material in this heating coil is somewhat longer, and the saponiflcation proceeds to a. considerable extent in the heating coil before the material is discharged into 'the zone 12.

'I'he aqueous glycerin which separates'from the fatty material in the zone 12 is removed through the outlet 18, the fatty material owing upwardly through the'tube 80 into the tray 82, which is quite deep, e. g. about 12 or 18 inches deep, and which serves as a separating zone for the aqueous glycerin or water owing downwardly through the vessel 10 from the top and the fatty material flowing upwardly through the tube 80. This zone or tray is also provided with petcocks 84 or other suitable devices for determining the position of the interface between the aqueous glycerin and l the fatty material therein, and the aqueous glycerin, which is the dilute glycerin solution resulting from the nal countercurrent saponification 'of the fatty material, is removed through the outlet 86. The upper portion of the vessel 10 may be provided with trays and is provided with a separating zone at the top and with an outlet for fatty acids and an inlet for water with much the same construction as the upper portions of the vessel 40 illustrated in-Fig. 1.

The .operation of the apparatus of Fig. 2 is similar to that of Fig. 1, the dilute aqueous glycerin from the countercurrent saponification of the partially saponied fatty material being advantageously used for the initial saponication of the fatty material, both the aqueous glycerin from the countercurrent operation and the fatty material being introduced into the heating coil 16, where the mixture is heated and the saponification is initiated. 'The temperatures 'maintained throughout this operation, and the pressures used, are much the same as those required in the operation of the apparatus of Fig. Lit being understood that the temperature within the zone 'l2 and the temperature within the rest of the vessell are maintained substantially below the temperature at which a single phase occurs, but sufliciently high to insure that the solubility of the waterin the fatty material is great enough to effect rapid csaponication. In the vessel 10 temperatures ranging from 200 C. to l250" C. or somewhat higher are advantageous, While the temperatures in the heating coil 16 may advantageously be somewhat higher, 'e. g. up to 265 C. or even higher, as it is not necessary t0 maintain separate phases within this heating coil.

All of thev apparatus, of course, should be erliciently insulated to prevent loss of heat, and the vessel 'lll may be provided with exterior unitary heaters suitably disposed to supply the heat which may be lost by radiation and for controlling the heating; or, if desired, the entire `vessel 10 may be jacketed and its temperature controlled by means of diphenyl oxide, high pressure steam, or other suitable heating medium.

In the operation of thisapparatus, as in the operation of the apparatus of Fig. 1, cold water may be introduced at the top, with the result that the fatty acids removed` are substantially free from dissolved water, the water being heated by contact with the hot fatty material, and

by heat suppliedto the vessel.

In Fig'. 3, there is illustrated a modification of a portion of the apparatus of Fig. 1. In this form of apparatus, instead of a single pressure vessel 24 for the completionvof the initial saponiiication, there is provided a plurality of vessels 88, and 92 (in the apparatus shown there are three of these vessels, but of course, the numcountercurrent treatment, as in the apparatus of Fig, 1, enters another similarvessel 90, advan tageously somewhat smaller, at the side. In thisl vessel, a continuation of the saponication and a similar separation of aqueous glycerin may take place, the aqueous glycerin being drawn off through outlet 96 and carried back to the first vessel. The fatty material from the top of this vessel then enters the third vessel 92 at the side and the process is repeated in this vessel.

i The fatty material is finally removed from the top of the third vessel and is led to a vessel similar to vessel of Fig. 1 for the completion of the saponication. The aqueous glycerin return lines 96 and 98 are provided with traps |00 and |02 to prevent circulation of fatty material through them.

Such an arrangement of pressure vessels avoids any short circuiting of the fatty materials and aqueous glycerin, such as might occur in the apparatus f Fig. 1 and insures an ample period of contact between the fatty material and the water or aqueous glycerin in the initial saponification.

Each of the pressure vessels 80, 90 and 92 are advantageously provided with petcocks |04 or other suitable indicating means at the sides to permit determination of the position of the interface between the fatty material and the aqueous glycerin, and all of the vessels should be efiiciently insulated to minimize loss of heat. The vessels may be jacketed or provided with unitary heaters to supply heat lost by radiation and to control the heating of the vessels.

Instead of operating in the manner just described, the third pressure vessel may be provided at the top with an inlet |06, through which hot or cold water may be introduced continuously or intermittently so that the saponiflcation of the fatty material may be completed without resort to a vessel similar to the vessel 40 of Fig. 1 for final countercurrent saponincation. In such case, the valve |08 in line 96 is closed, so that the aqueous glycerin from the pressure vessel 90 does not flow back into the pressure vessel 08 and the aqueous glycerin from the vessel 90 is Withdrawn through the outlet I|0 controlled by the valve H2. The aqueous glycerin so removed is advantageously introduced into the initial heating coil (not shown in this figure), along with the fatty material to be saponifled.

In the initial part of my process, the saponification is not a complete saponiiication of some of the triglyceride molecules leaving the other triglyceride molecules unsaponiiied, but rather is to a large extent a .partial saponication of some of the triglyceride molecules, Ilrst into fatty acids and diglycerides along with remaining triglycerides, the amount of diglycerides present gradually increasing while the amount of triglycerides decreases. As the saponication proceeds, and with higher percentages of fatty acids set free from the fatty molecules, there is a simultaneous formation of monoglycerides by the further saponiflcation of diglycerides, and the proportion of the unsaponied matter remaining as monoglycerides after substantially 60% saponiflcation has been reached is very large. It may thus be readily understood that the nal portion of my process, following as it does a very substantial degree of saponication which leaves a high percentage of monoglycerides in the partially saponiiied fatty material, with corresponding lower amounts of diglycerides and triglycerides, is substantially diiferent from other types of saponiflcation that have been described and which employ triglycerides as fatty materials.

It has been found that monoglycerides, unlike triglycerides, have a strongtendency to emulsify with aqueous liquids and for this reason I find it important to provide means, such as hereinbefore described, for separating partial emulsions at the points where aqueous glycerin aolutions and fatty acids are withdrawn from contact with one another, as well as means to minimize emulsion of the aqueous and fatty phases.

I have described the operation as a continuous process, with water and fatty material ooninuously introduced into the apparatus in proper amounts, and proper proportions; and I prefer to operate the process in such continuous manner. Nevertheless, the process and apparatus may be operated in an intermittent or semicontinuous manner, withintermittent or alternate introduction of water and fatty matreial, within the scope of my invention in its broader aspects. Also, while I have described the invention as one involving the` hydrolysis of fats and fatty oils by the use of liquid water alone, at high temperatures and pressures, it should be understood that if desired, and if unobjectionable, suitable catalysts may be used to speed up the hydrolysis.

I claim:

1.The method of hydrolyzing fats and oils which comprises concurrently heating the fatty material with liquid water to temperatures in excess of about 185 C. for a sufficient length of time to effect a substantial degree of hydrolysis, thereafter maintaining the temperature so that it is above 185 C. but substantially below about 287 C., separating the resulting aqueous glycerin from the fatty material, and completing the hydrolysis of the fatty material by bringing it into contact with successive portions of liquid water at temperatures above about 200 C. but below the temperature at which a single phase is formed at a pressure substantially above the pressure of saturated steam at the highest ternperature employed, while minimizing emulsication of said fatty material with said successive portions of liquid water with which it is brought into contact.

2. The processv of hydrolyzing fats andA oils which comprises bringing the fatty material and aqueous glycerin to substantial equilibrium at a temperature above about 200 C. and substantially below 287 C. at a pressure suiiicient to keep the water in a liquid phase, separating the resulting aqueous glycerin from the fatty material and completing the `hydrolysis of the fatty material by bringing it into contact with successive portions of liquid water at temperatures above about 200 C. but below the temperature at which a single phase is formed and at a pressure substantially above the pressure of saturated steam at the highest temperature employed, while minimizing emulsification of `said fatty inaterial with said successive portions of liquid water with which it is brought into contact.

3. The method of hydrolyzing fats and oils which comprises concurrently heating the fatty material with liquid water to temperatures in excess of about 185 C. for a sumcient length of time .to effect a substantial degree of hydrolysis, thereafter maintainingthe temperature so that it is above 185 C. but substantially below about 287 C., separating the resulting aqueous glycerin from the fatty material, andcompleting the hydrolysis of the fatty material by bringing it into countercurrent contact with liquid water at temperatures above about 200 C. but below the temperature at which a single phase is formed and at a pressure substantially above the pressure of saturated steam at the highest temperature employed in said countercurrent operation.

4. The process of hydrolyling fats and oils which comprises bringing the fatty material and aqueous glycerin to substantial equilibrium at a temperature above about 200 C. and substantially below 287 C. at a pressure sufficient to keep the water in a liquid phase, separating the resulting aqueous glycerin from the fatty material Aand completing the hydrolysis o-f the fatty material by bringing it into countercurrent contact with water at a temperature above 200 C. but below 'the temperature at which the water and the fatty material form a single phase, and at a pressure substantially above the pressure of saturated steam at the highest temperature employed in said oountercurrent operation.

' 5. The process as in claim 4, in which the dilute aqueous glycerin obtained from the countercurrent hydrolysis is used Ato effect the initial hydrolysis of the fat or oil.

6. The process of hydrolyzing fats and oils, which comprises heating a fatty material and dilute aqueous glycerin in intimate concurrent contact with each other to a temperature sufficiently high, and for a period sufdciently long, to effect a substantial degree of hydrolysis while maintaining aV pressure sufficient to prevent vaporization of water, separating the resulting aqueous glycerin froml the fatty material while maintaining the temperature substantially below 287 C. and while maintaining the high pressure, and completing the hydrolysis of the fatty material by bringing it into intimate contact with successive portions of watercat a temperature above about 200 C. but substantially below about 287 C. and under a pressure sufcient to prevent vaporization of the water.

7. The process of hydrolyzng fats and oils which comprises heating `a fatty material and dilute aqueous glycerin in intimate concurrent contact with each other to a temperature sufficiently high, and for a period sufficiently long,

toeifect asubstantial degree of hydrolysis while maintaining a pressure sufficient to prevent vapoi-ization of water, separating the resulting aqueous glycerin from the fatty material while maintaining the temperature substantially below 287 C. and while maintaining the high pressure, and completing the hydrolysis of the fatty material. by bringing itinto intimate contact with water by countercurrent iow at a temperature above about 200- C. but substantially below about 287@ C. and under a pressure sulficient to prevent vaporization of the water.

8. The process as in claim 7 in which the aqueous glycerin used for the initial hydrolysis is that resulting from the countercurrent hydrolysis.

,9. The process of hydrolyzing fatty materials -which comprises concurrently heating the fatty it into contact withsuccessive portions of liquidv water at a pressure substantially' in excess of the pressure of saturated steaml at the highest temperature employed and at a temperature above about 200 C. but below the temperature at which a single phase would result.

10. The process of hydrolyzing fatty materials which comprises concurrently heating the fatty materials with dilute adueous glycerin containing not more than about 15% glycerin to a sufflciently high temperature and for a suiiiciently long period of time to effect a substantial degree of hydrolysis, separating the resulting 'glycerin solution from the fatty matter at a temperature substantially below 287 C. and subjecting the fatty matter to a further hydrolysis by bringihg it into countercurrent contact with liquid water at a pressure substantially in excess of the pressure of saturated steam at the highest temperature employed andat a temperature above about 200 C. but below the temperature at which a single phase would result.

11. The process as in claim l0 in which the initial hydrolysis is continued for a length of time such that the fatty material after this initial hydrolysis contains at least free fatty acids.

12. A method for the aqueous saponication of fatty material which comprises concurrently heating the fatty material. and liquid water in contact with one another, under sufficient pressure to prevent the vapor-ization of water, said water being employed in amounts in excess of 10% of the weight of fatty material, to temperaltures in excess of about C. until a substantial degree of saponication is effected, separating the resulting aqueous glycerin solution from the fatty material at a temperature substantially below about 287 C. while maintaining the high pressure, and subjecting the fatty material thus separated to contact with successive portions of liquid Water at a temperature substantially below about 287 C. whereby a further saponication of the fatty material is effected.

13. A method for the aqueous saponication of fatty material which comprises concurrently heating the fatty material and liquid water in contact withV one another, under sufficient pressure to prevent thevaporization of water, said Water being employed in amounts in excess -of 10% of the weight of fatty material, to temperatur'es in excess of about 185 C. until a substantial degree of saponication is effected, separating the resulting aqueous glycerin solution from the fatty material at a temperature substantially below about 287 C. while maintaining the high pressureand subjecting the fatty material thus separated to' countercurrent contact with liquid water at a temperature substantially below about 287 C. whereby a further saponication of the fatty material is effected.

14. The method for the hydrolysis of fatty material which comprises concurrently heating the fatty material and dilute aqueous glycerin in contact with one another, under pressure, the amount of water in the aqueous glycerin being at least 10% of the weight of the fatty material taken, until a substantial degree of hydrolysis is effected, separating the resulting aqueous glycerin solution from the fatty material at a temperature substantially below about 287 C. while maintaining the high pressure, and subjecting the fatty material thus separated to countercurrent l contact with liquid water at a temperature substantially below about 287 C.- whereby a further hydrolysis of the fatty materials is effected.

15. The process as in claim 13 when carried out continuously under pressure.

16. The process as in claim 14 when carried out continuously under pressure.

17. 'I'he method for the hydrolysis of fatty material which comprises concurrently heating the fatty material and dilute aqueous glycerin in contact with one another, under pressure, the weight of water in said aqueous glycerin being at least 10% of the weight of the fatty material taken, and the concentration of glycerin being below about 15%. to a suillciently high temperature and for a suillcient length of time to effect a substantial degree of hydrolysis, separating the resulting aqueous glycerin from the fatty material at a temperature substantially below about 287 C., and bringing the separated fatty material linto countercurrent contact with liquid water at a temperature substantially below about 287 C. and under a high pressure substantially in excess of the pressure of saturated steam at the temperature selected, wherebyfurther hydrolysis is eifected.

18. The process as in claim 17 when carried out continuously under pressure.

19. The process as in claim 14 in which the aqueous glycerin resulting from the countercurrent contact of the fatty material with liquid water is employed as the aqueous glycerin used for the initial hydrolysis of the fatty material.

20. The processes in claim 14 in which the amount of water in the aqueous glycerin employed in the initial hydrolysis is in excess of 30% of the weight of the fatty material taken, and the amount of glycerin in said solution does not exceed about 15%, and in which this aqueous glycerin is that resulting from the countercurrent contact of the partially hydrolyzed fatty material with liquid water.

21. The process as in claim 14 in which the initial hydrolysis is carried out to an extent Such that the separated fatty material contains at least free fatty acids.

22. 'I'he process as in claim 14 in which the initial hydrolysis is carried out to an extent such that the separated fatty material contains at least free fatty acids.

23. The process as in claim 14 in which the 'initial hydrolysis is carried out to an extent such that the separated fatty material contains at least free fatty acids.

24. The process as in claim 14 in which the initial hydrolysis is carried out to an extent such that the non-hydrolyzed portion of the fatty material separated from said initial hydrolysis consists largely of monoglycerides. 1

25. In the aqueous saponification of fats and Oils at high temperatures and pressures, the steps which include heating the fatty material in contact with water to a high temperature for a suiliicient length of time to eifect a substantial degree of saponiiication, separating the resulting aqueous glycerin from the fatty material at a temperature substantially below 287 C. while main-A taining the high pressure, and cooling the aqueous .glycerin to eiect the separation of dissolved fatty'material therefrom while maintaining the high pressure, whereby aqueous glycerin substantially free from fatty material is obtained. A

26. In the continuoushydrolysis of fats and oils by concurrent heating of the fat or oil and water or aqueous glycerin in contact with one another under sufficient pressure to prevent yaporization of the water, the steps of separating the glycerin solution formed from the fatty material at a temperature substantially under 287 C. while maintaining the highipressure and cooling the separated glycerin solution to a temperature substantially below the temperature of the greater part of the fatty matter to eiIect the separation therefrom of dissolved fatty material before releasing the pressure from said separated glycerin solution.

MAR'I'IN H.

CERTIFICAIE oF CORRECTION. Patent No. 2,221,799. November 19, 19m.

MARTIN H ITTN'ER.

It is hereby certified that error appears vin the printed specification of the aboveV numberedpatent requiring correction as follows: Page l, first column, lines 27 and 28, strike out the words "is used but in which the saponification or hydrolysis"; and second column, line 'J2-55, for solbility read --solubility; page 2, first column, line 5l, before "90%" insert -to-; ima 57, after the sy11ab1e "ed" strike out' the coma; une 7o, for 50101 read #-50% or; same page, second column, line 67, after "material" strike out the commafpage 5, first column, line 5l, after "C." strike out the comme; page 7, lsecond. column, line 5-6, for "coninuously" read continuously-q line l2, for "matreial" read msterisl; line 55, claim-l, after "formed" insert -and-; page `8, second column, line 66, claim lli, for the word "materials'f read --mnterielmq and that the said Letters Patent should be read with this correction therein that thesame may conform to the record of the case in the Patent Office. i

Signed and sealed this lith day of February, A. D. 191;.1.

Henry Van Arsdale,

(Seal) Acting Commissioner of Patents. 

